Hydrocarbon conversion and fractionation system



Apllrl, 1946- w. c. EDMISTER ET AL 2,398,496

HYDROCARBON CONVERSION AND FRACTIONATION SYSTEM Filed March 31 PatentedA-pr. 16, 1946;

HYDROCARBN? CONVERSION AND FRACTIONATIONI SYSTEM i Wayne C. Edmister; Flossmo'or, and.4 Doyon H.

Pollock, Chicago,- Ill., assignorsA to. Standard-Oil` Company', Chicago,v Illi, alcorporation oflmiana i 'Application March 31, 1942, SeriallNo. 437.048 6 Claims. (Cl. 13G-52) u y This invention relates toimprovementsin a hydrocarbon conversion-and. fractionation system and it pertains more particularly to an improved method and means for controlling the operation of a fractionation system which is designed normally to handle hydrocarbon vapors of relatively low averagev boiling point and'which may be calledr upon from time to time to handle' hotter hydrocarbons of higher average boiling range, The invention will be describedin connection. with a -uid type catalytic crackingsystem employing powdered catalyst but it should be understood that the invention` is not limited' to catalytic Vcracking systems or to powdered catalyst conversion .systems since many features ofthe invention are applicable to hydrocarbon fractionation sys-- tems generally. Q y l In the fluid-type catalytic cracking'process the charging stock is vaporized in a pipe still, thehot vapors pickk up powdered catalyst from the base of a standpipe and carry thecatalyst in suspension into a reactor, and reactionvapors from the top of this vreactor enter afractionating column; After separation from reaotionvapors, thecataf lyst'is suspended in a regeneration gas andre' generated in a regeneration chamber. After separation from regeneration gases the regenerated catalyst passes downwardly through the standpipe and lis picked up byadditional charging stock y vapors. n v

ItV is importantin suchfluid type systems to prevent the hot charging stock vaporsv from owing upwardly through the standpipe and into; the

regenerator. Usually" the standpipe'is of` such height that the aerated catalyst pressure 'at'. its

higher than the pressure in the pipe still transfer line. If for any reason there is a loss ofpressure head inthe standpipe avalve is automaticallyv closed in the transfer line leading tothestandpipe andl a valve is automatically opened ina-by-pass line so that the charging stock vapors arefintroV duced directly from theA pipe still to the fractionv ating column.

For normal .operation the fractionatingcolumn may be designed to handle about 11,230 barrels per day of 50.2 degrees A. P. I. gravity (all A. P. I. gravities are those measuredat 60 F.) hydrocarbons which are introduced near the base ofthe column in vapor form at a temperatureof about 900 F. anda pressure of about 6 pounds per square inch. When the reactor is by-passedthe inlet stream to the fractionating column may be about 10,500 barrels per day of a"30.5 degree A. P. I. hydrocarbon stream which Vis vaporized and. heated to a temperature` of approximately 950av F; The objectof our invention isto provide methods and: means. whereby the fractionating' system will functionV smoothly and properly in this by-pass operation A further object" is "to prevent product streams from becoming` contaminatedduring` by-pass operation. A further objectis to'. provide a-system which willpromptly resume normal operation when the reactorlsfonce r more placedV on-stream, A'further` object is to make 'by-passing operation as nearlyv automatic and foolproof Vas possible l sol that plant operators maydevotetheir` attention to. the catalyst! flow difliculties that madel the by-passing-` necessary. A furtherv object is to'utilize all ofthe equipment available for normal'operation` as: emciently" as.

possible vduring byfpass operation an'dtolminimize additional equipment; required for bypass operation;

Vbase will be about 1 to 5 pounds per square' inch `average boiling point` hydrocarbons.

Al further objectofthe invention is to provide improved methods and 'means for operating a` fractionating column which mayA be suddenly calledupon to handlefhydrocarbon vapors which are hotter 'andi of higher!vv average boiling point than those" for.` 'whichthecolumn is designed" to" normally operate. `A further object isitovpro'- y vide improved methods and'means vfor decreasing the amount of heat abstracted from the topof the column during emergencyoperation. A further object is tov provide` improved methods and means for preventing liquidlevels in a fractionation columnfrom exceeding predetermined iev-i els'when the columniis suddenly called uponto handle `hotter vapors of` higher average boiling point hydrocarbons. Afurther object is to `provide improved metho'ds andmeans for preventingfproduct-contamination by heavier hydrocarbons when a fractionatingf column is suddenly called Vupon to handle hotter vapors ofhigheraverage boiling pointhydrocarbons.-

Afurther` object'is` tomaintain a positive pressureon the compressor inlet during emergency operations when the normal supplyl of gases to the compressor is discontinued; A further object is to provide one ormore controls for'emergency operation which will render the` normal tower temperature-controls ineffective when the tower is called upon to handle hotter vapors of higher Other objects will beapparent as the detailed description of the inventionproceeds.

In practicing our invention we employ atleast one and preferably at least two liquid level controllers in the fractionating tower. We provide a liquid level controlled by-pass'on the tower top reflux'stream and a liquid level controlled valve for regulating the withdrawal of heavy oil from vthe total trapout pan in the intermediate section of the column. We may employ a liquid level controlled by-pass on a cooling stream near the bottom of the tower. We may provide automatic means responsive to a liquid level in the tower or to tower temperature or other operating conditions for automatically closing of product lines and opening slop lines in place thereof.

In emergency operation the tower top temperature regulator is automatically renderedl ineffective by the tower top reflux by-pass. Gases from an extraneous source are introduced/into a stream leaving the top of the column for maintaining a positive pressure at the compressor inlet and these compressed gases may be recycled during the emergency operation. The fractionating column will operate throughout at a higher temperature so that the charging stock will be preheated to higher temperature and the hotter charging stock will automatically bring about a reduced amount of heating in the pipe still because the pipe still burners are automatically controlled by the inlet temperature of the charging stock. Y

.Briey, the sequence of operations when, the reactor is by-passed is substantially as follows:

(l) When going onto by-passing-operationan appropriate amount of additional surface, on the tower bottom reflux system is brought in service -by the Esame valve mechanism which by-passes the reactor. Thus the reflux duty in the lower section is increased and the liquid level in the base of the tower begins to rise tending to open the by-pass valve around the cooler. This cooler bypass valve is set so that it may not open beyond a certain predetermined point, in order that the flow through the coolers is never below a certain vpredetermined quantity. Thus the liquid level continues to rise .upY to the operating range of the upper of the two lower liquid level controllers.

(2) This liquid level ycontroller may initiate the withdrawal ofxliquids from the bottom of the Vtowerand from the intermediate total trapout pan to slop (charging stock tanks).

(3) The liquid level in the intermediate part of Athe tower will tend to rise and the liquid withdrawal of gas oil `atvthis point will be increased.

(4) As the liquid level in the intermediate part of the tower continues to rise a by-pass will be opened in the tower top circulating reux stream so that although substantially the same quantity of liquid is circulated in this stream, it will be returned to the tower at a much higher temperature andA will thus allow the temperatures in the column to rise; during this operationv the temperature controller on the tower top circulating reflux stream will be rendered ineffective by the by-pass'- ing of said stream around the normal coolers and light gas oil drawoi and liquid overhead products may be diverted to slop. Y Y 'y (5) The pressure at the top of the column will decrease and the pressure control valve vacuum breaker will automatically open and admit reiinery fuel gas. A

(6) The load on the gas compressor will decrease and suction valve unloaders will open, permitting the compressor to idle satisfactorily for a few minutes until the operator can open the gasY recycle line.

(7) If not already accomplished the light gas oil going overhead and hot products will bediverted to slop.

(8) The charge to the furnace will be preheated to 550 F. instead of 450 F. by heat exchange and the transfer line temperature control at the furnace will accordingly decrease the furnace firing to maintain the same transfer line temperature.

When normal operation is resumed the by-pass lines around'coolers in the fractionation system will be closed and after thenecessary time interval the product lines will be again opened and the slop lines closed. The system may thus be expeditiously-and quickly brought back to normal conditions with a minimum of time and eort. l

At least one of the emergency control valves should be automatically opened in response to an undue rise in the liquid level in the fractionating column. When the first control is automatic sufcient time may be provided for operators to manually attend the remaining controls under ordinary conditions. However, we prefer to employ a system which is as automatic and foolproof as possible and which will permit the operators to devote their time and energy in rectfying difficulties in the catalyst system.

The invention will be more clearly understood from the following detailed description read in conjunction with the accompanying drawing y which forms a partof the specification and which isr a schematic flow diagram illustrating one embodiment of our improved conversion and fractionation system.

While certain aspects of our invention are in no way limited to hydrocarbon conversion processes or to the use of catalysts either in. powdered form or in the form of xed'or moving beds, we will describe the invention-as applied to a fluid type catalytic cracking process employing a powdered silica-alumina catalyst and converting 30.5 degrecs A. P. I. gravity gas oil to substantial yields of a high quality motor fuel.

The catalyst in this particular example is preferably of the silica-alumina or silica-magnesia type. This catalyst may be prepared by the acid treating of natural clays, such as bentonite, or by synthetically preparing a silica-alumina or silicamagnesia mixture. f An excellent catalyst may be prepared by ball-milling silica hydrogel with alumina or magnesia using about 2 to 30%, for example about 15 or 20%., of alumina or magnesia. The ball-milled dough may be dried at a temperature of about 240 F. and then activated by heating to a temperature of about 900 to 1000" F. Another method'of preparing a highly active cracking catalyst is to form a gel from dilute sodium silicate in the presence of an aluminum salt by the addition of excess dilute sulfuric acid. The resulting gel is preferably boiled for an hour or two with an excess of dilute ammonia hydroxide solution before washing, after which it is dried and heated as in the previous example. Thesilica-alumina catalyst may be rendered more stable at yhigh temperatures by the addition thereto of zirconia in either smaller or larger amounts than alumina. The ball-milled silica-magnesia catalyst may be improved bypreheating the magnesia with a thorium nitrate solution so that the finished catalyst may, for instance, have the' following composition:

. Per cent Silica 66 Magnesia 27 Thoria 7 sity of the dense phase catalyst in this reactorv may be about 18 pounds per cubic foot. The vertical velocity of the upflowing vapors in the reonly that the catalyst be of such size and density may be in the general vicini of 10 minutes so a it may e aerated and handled as a duid in that the wei ht space velocity will be in the genemanner herein described Higher gas or vapor eral vicinity of a out two parts by weight of velocities may e required for coarser catalyst c arging stock introduced per hour per part b particles, but these particles may be of such size weight of catalyst in the reactor at any instant as to-be retained on a 400 300, 200, 100 50 or even l0 S eain ma introduced into the charging stock mesh sere during the heating step or after the heating step he density of the catalyst pai ticles per se may and steam may be employed for dispersing cataas high unds per cubic foot but the lyst in charging stock vapo bulk density of catalyst which has settled for 5 to the upper part ofthe reactor we may pro- 1 minutes will usually be from 25 o 40 pounds l5 vide a `funnel-shaped top` 23 terminating in an per cubic oot With slight aeration i e, with upwardly extending conduit 24 so that suspended vapor velocities of about 05 to .5 foot per second catalyst is carried upwardly and deflected by e bul density of 1-100 micron catalyst will be baille 25 into settling chamber e may, howabout to pounds per cubic foo With vapor ever, completely eliminate this u per part of the velocities of about l to 2 or 3 feet per second the 2o -reac'tor and wit draw catalyst directly from the bulk density of such catalyst may be about 10 to ense phase in the reactor as will be hereinafter 0 pounds, for example, about 15 to 18 pounds per pointed out. Gasses from the upper part of the cubic foot is a such gas or vapor velocities enlarged settling chamber pass through conduits at powdered catalyst is maintained in the 1 into primary cyclones 28 from which separated dense, turbulent suspended catalyst phase At 25 catalyst is returned to the base of the settler higher vapoi velocities or in settling zones the bulk through dip leg 29. Gases from the primary cydensity of catalyst may be less than pounds per one are conveyed by`conduit 30 secondary cubic foot oneven less than 1 pound per cubic foot cyclone 3| and catalyst separated therein is reand it is under such conditions that the catalyst turned to the base of the settler through dip lesr is said to be in the light, dispersed phase The 32 Gases and vapors leave cyclone 3| through dilute phase may contain as little as 50 grains per conduit 33 and are introduced into tertiary cycubic foot Generally speaking, the catalyst in clone 34 which is provided with dip leg 35 Re e dense, turbulent suspended catalyst phase has ac on gases and vapors-leave the tertiary cyclone a bullk density of 1 to 5 and preferably of at least through lines 35 and are conveyed by line 31 to a 1 pounds per cubic foot greater than the bulk 35 low point in tractionating column or tower 38. density of the light, dispersed catalyst phase Settled catalyst leaves the base of settling Aerated catalyst in the overflow pipes oi standchamber 26 through standpipe 39 which is aerated pipes,- even while undergoing stripping, may have and stripped by steam introduced through line the bulk density of 20 to. 30 or more pounds per Additional stripping steam may be introcubic foot, i; e., at least 1 and preferably 5 pounds 40 duced directly in the base of the settling chamber per cubic foot heavier than tliedense, turbulent t roug line a pent catalyst is discharged suspended catalyst phase. from the base of standpipe 39 in amounts reguout 10,00 arrels per day of a gas oil charglated by valve 4I is picked up by air introduced ing stock from source I0 is introduced by pump through hne 42 an is conveyed by line 43 to the y II through line I2, heat exchanger I3, heat exbase of regenerator44. e construction rand changer I4 and heat exchangerv I5 into coils I6 operation of the regenerator is similar to that of pipe still furnace I1. An additional 500 brarhereinabove described for the reactor except that rels per dayof recycle slurry is also introduced the regenerator maybe three or four times as through lines 52 to furnace coils I6 e chargarge as the reactor .'Iheseparation system cying stock may be partially or completely vapoiclone separator etc., will, therefore, not be deized in the pipe still coils and heated to a tians scribed in further detail. Regeneration gases fer line temperature of approximately 950 F. at a leave the regenerator through line 45 and may be transfer line pressure in the general vicinity of passed through a heat exchangeror flue gas cooler a out 15 to nds r square inch gauge. to an electrostatic precipltator for the recovery of ot regenerated catalysty in standpipe I9 is aer- 'i5' additional catalyst nes. Make-up catalyst may ated by steam introduced byline 20 and this aerbe introduced directly tothe settling chamber ated catalyst is introduced in amounts regulated above the regenerator as required. by valve 2I into transfer line I8 to give a catalyst- Temperature control in the regenerator may o-oil weight 'ra 'o of approximately 3 1 to 4 l. be effected by withdrawing a stream of regenerhe pressure at the base of the standpipe may ated catalyst through standpipe 46 which is e about 19 or 20 pounds per square inch so that aerated by air introduced through line 41 'l his there will be a pressure diierential of about l to 5 Withdrawn catalyst may be discharged from the pounds perv square inch across valve 2I This base of the standpipe in amounts regulated by prevents the hydrocarbon vapors from passing valve 48 picked up by air introduced through upwardly through standpipe I9 into the regen- 65 line and conveyed' through cooler 50 back to eration system. i 4 the regenerator Alternatively, temperature conhe charging stock vapors together with susrol may be effected by the use of a Stirling boilci pended catalyst are introduced at the base of or other heat exchange means directly within the ieactor 22 which may be a cylindrical vessel about regenerator. Additional regenerator air may be 12 to 13 feet in diameter by about 25 feet in 70 introduced through line 5I. Regenerated cataheight and which may operate at a base pressure lyst is Withdrawn through line I9 as hereinabovn of' about 13 pounds per square inch and a top described. pressure of about 8 to 10 pounds per square inch When the cone-shaped top is omitted from the and at a temperature of about 900 F. The denregenerator we may substitute standpipe I9 for standpipe 19,1. e., we withdraw regenerated cataexchanger 56 V-ticles may be About 2,510 barrels per day of through line 15.

lyst directly from the dense turbulent suspended catalyst phase either from the bottoml of the regenerator or from an intermeditae point therein. Similarly when the funnel-shaped top of reactor` 22 is omitted we employ standpipe 39' in place of standpipe 39. In such cases the cyclone dip legs may be extended so that they terminate within the dense phase within the reactor or regenerator or we may so operate that the dense phase extends into the base of the enlarged separation phase levels are high employ standpipes |9 the base and be provided with inclined cilitate the scrubbing out lyst material from the upflowing vapors. 500 barrels per day of the heaviest condensate together with about 800 pounds per hour of catalyst and coke may be withdrawn from the base of this scrubbing section of the column through line 52 and returned by pump 53 to line-|2 or to one or 4more of the coils I5 in pipe still furnace |1. In normal operation about 21,000 barrels per uday ol heavy 20 degree A; P. I. gravity `condensate leaves the Vbottom of the tower through line 54 at a temperature of about 550 F. and is pumped lby pump 55 through heat it is cooled to about 533 wherein it is cooled to exchanger 50 wherein F., heat exchanger |5 about .457 F., thence F.. and to cooler 59 wherein it is cooled to about 380 F. the cooled stream being returned byline 50 to a'point in the column above the pointof vapor inletV During normal operation no product stream is withdrawn at thisfpoint. Aby-pass line 5| is provided around and l5; since solid catalyst parsuspended in the liquid withdrawn through line 54 it isimportant that provision be made for continuouslycirculating said liquid and preventing these solids from settling out when it becomes necessary, for example, to clean one of the exchangers.

At an intermediate point in vide a total liquid trapout heavy gas oil which is withdrawn atthe rate of abouty 5,015 barrels per day by pump 64. This heavy gas oil stream enters exchanger I4 at about 420 F.. leaves heat exchanger |4`at about 275F. land leaves heat exchanger 65 at about 140 F. this cooled gas oil passes through cooler 06 wherein it is cooled to about 110 F. and used to supply the oil for pump glands |51 in thesystem. This gland oil is returned to the column through line 68, about 1,060 being introduced through line 59 g plate 62 and about 1,510 barrels per day being introduced above the trapout plate through line 10. Gland oil may by-pass the pump glands through the tower we propan 62 for 25.6 A. P. I.

the upstream sideof the pump glands exceeds av predetermined maximum. The withdrawal of heavy gas oil isv regulated by 'mains closed until the'liquid level control 13 operates through means 14 to open said valve 12; lthis is for maintaining the necessary amount of gland oil in the system and' for insuring the required amount of lcharge for pump 64. 'In normal operation about' 2,445 barrels per day'oi 25.6 A. P. I. gas oil is withdrawn from 'the system line 1| if the pressure in line on "out'plate 16, 16' or by-passed by Aof heating at this point.

, per day o temperature of y about 250 n 51 to heatA exchanger 58 wherein y it is cooled to about395 arator 98 duced to the stripper 'about4,190 barrels per day of 36.8

.through line 92 lgasoline stabilizer system ,.4 from line I l2 may be sent to an absorption System Valve re.. t..

oil stream is withdrawn from trap- 16" and introduced byline 11 into side stream stripper 18. About 3,180 barrels per day'jof 31 A. P. I., gas oil is thus `introat a temperature of vabout F. vFrem trapout plate 19in the stripper A. P. I. oil is picked up by pump and passed by line 8| through heat'exchanger 55, this stream entering the heat exchanger at a temperature of 400 F. and leaving theheater at about turn to the base The heat'exchanger may be partially or entirely line 83 to obtain the desired amount A light gas at vthe base of the stripper from the 5;. a

P. I. gasoil is thusA removed from the system. yOverhead from side stream stripper-18 is returned to` the column through line 81.

Near the vupper part of the tower we provide trapout, plate 88 from which about 41,000 barrels f 45 A. P. I. reflux is withdrawn at a F. by pump 89`through line 90.' rIhis tower topreflux stream leaves heat exchanger |73 at about 227 F., leaves cooler 9| at about 150 ,F., and is returned to the tower top at that temperature. A throty operated by temperature controlled means 94 in order to maintain a substantially constant .temperature inthe overhead products leaving the tower top through line 95.

About 3,960 barrels per day of 57.0 A. P. I. gasoline and about 2,200 cubic reetper'mi ute of gases (measured at standard conditions) leave the tower through line 95 at about 230 F., leave condenser 96 at about 120 F. and leave cooler 91 at about 80" F. at which temperature the stream is introduced into separator 98.' Water is withdrawn 'from' thel base of this separator through line 09, uncondensed gases .are taken overhead through linev |00 tothe dry drum |0| from the base of which any entrained liquid is separated from the'vapor and withdrawn through line |02. Gases leave `the top of drum |0| in line l|03 which leads to the inlet side of compressor |04. The condensed gasoline iswithdrawn from sepy through line |05 and pumped by pump |00 vthrough line |01 to line |08 leading from the discharge side of, gas compressor |04. The combined gas-.gasoline streamthen passes through cooler |09 andis introduced into surge drum |10 from which unstabilized gasoline and wet gas are removed through lines H4 and H2 respectively for f rther processing. Water may be withdrawn from drum ||0through line Uncondensed gases or vapors may be withdrawn from the top of surgev drum |l0through line I2. The fraction 1s removed through line H4 by through line H5 to a (not shown). Gases tling valve 9 3 is (not shownlvia line ||1a.

VDuring starting up periods gases from line I2 may be vented to a blow-down tank through line ||1 and similarly gases from line |00 may be vented to a blow-down tank through line H8. Thus far wefrhave described the normal operl ation ofthe fractionation system while the reactor is on stream.

l If the pressure differential across valve 2|'. in

standpipe I9 (or valve 2|. in'

A. e. I. gas' oir wmlbe withdrawn fi-om the sysl t standpipe I8?) should fall below `a predetermined minimum, automatic means leading to'valve control mechanisms I2| eiect the automatic closlng of valve l|22 and opening of valve |23 so that the hot gas oil vapors by-pass the reactor and are introduced directlyto a low pointin the fractionating column throughline |24." 4The valve control mechanisms |2|` may be of the type illustrated by the regulating meansv 12 shown in U. S.

Letters Patent 2,081,398, means |20 :being of the manometer type connected acrossvalve 2|, and valves |22. |23, etc., being pressure operated in the mannerdisclosed in said patent. Alternativetem through slop line |35. i

In this by-passingV operationabout 3200 barrels per day of 34.2 A. P. I. gas oil will be withdrawn through line 1T atabout 480 F. to jside stream stripper 18. The temperature controlled means in by-pass line B3 will cause a short circuiting of heat exchanger 56 sothat no additionalheat will be supplied atthe base of the side stream stripper. The-same amount of steamlmay be introduced at the base of this stripper during thev emergency 'operation as duringnormal op-` eration; 'About 2,445 barrels per day of`33fl ly, the control means may be electrically operated'A or theymay be manually orieratedy in accordance with anindicated pressurediiiere'ntial across valve 2| or 2|. Control mechanism I2| ralso opens valves putting cooler iu'into service thus increasing the cooling capacity` of the slurry reiiux system. In such an emergency` operationYV the fractionating column is suddenly called upon to handle 30.5 A. P. I. gasoil vapors introducedV at a temperature of about 950 F; (insteadof 50.2

A P. 1. product vapors at 90o.d FJ.. The liquidy level will immediately tendto rise in the base of Ycolumn 38. The rst effect this risng liquid llevel is to actuate liquid level Scontroller |25 and by suitablemeansll responsivefto this liquid level controller, valve'I21 in.zby`pass line |28 is opened to a predeterxninedpoi'xit whi cl1A may be adjusted by a-,stcjn-f-f-on-the,iristruinenuv Under these conditionsthere-'is an of reflux duty in the scrubber section 'and consequently thefli'q-` Y uid levelinfthe base of thetowergradually As the liquidlevel-continues to rise in the base of column 38 liquidlevel controller |29 will func-` tion through suitable means I`to` open valve |3I in slop line |32 so 'thatvabout 2,500 barrels'.

per day of gas oil is removedfto'slop tanks from base of the column.' lThe means for opening valvek I`3I may be automatically controlled by liquid levelcontroller |520', meansmay automatically close valve |33 and open; valve |34 so that the heavy gasoil strearnvwill/be diverted from line 15to slop line |35. In this operation about 22,000.1;arre1sperv day oi 25.2 A. P. I. gas' oil leaves the base of the towerthrough line 54 for recirculation by pump 55. This stream leaves heat exchanger 56 at about the same temperavture and leaves heat exchanger I5 at about 582 F. The boiler feed water heatexchanger may be substantially ineffective and, in fact, it may be by-passedby line |28 as--the demand for boiler feed water decreases so that a partl of the stream from line 51 passes through cooler 59 which is now called upon to removeabout iive` times as much heat asduringV normal opera'- tion. The streamreturned to line 60 willnow be t at a temperature rof about 510 F. v

' 180 F. About the same amount ofgland 'oil will be required'A and this oil will leave cooler (itV at about F. About 3055 barrels per day of 28.9

A. P. AI. gasoil may be `withdrawn from the system throughjslop line |38. thiswithdrawal being t automaticallybrought about by liquid` level indicator |42 throughsuitableactuating device I42a responsive` to-the Increased liquid level which automatically closesvalve |36k and automatically 20 opens valve |31 thusdiverting light gas oilsfrom product line 06-to slop-line |13. Similarly valve |39v may` be automatically closed and valve |40 may be automatically opened to by-pass the overhead streamfrom gasoline stabilizer to slop line I4I. If desired. we 4may eiect this by-passing to line IIdinstead airline |01.: g

The redux-stream withdrawn by pump 89-may be the same in Volumens in the case of normal `operation but -thestream willbe removed from l the tower at a ,temperature ofabout 395 F. and

it wiuof about 36 A. i?. I. gas on. i About 8130- barrelsper otjths stream Will leave exchanger vI3 ata'tem 'atureof about-263 and will leave vcoolserlgl4 .a temperature of about 96 Fgsothat-thestreanr-willfbe returned vto the top of the column through line' 92st a temperature of about 350F. lit-should benoted that` in this operation bye-pass; line renders the temperature controlled throttle valve` 93 ineffective. lThus the various streams :from the fractionating column may thus ybe automatically transferred from product streamsto slop line streams in accordance with liquid level indicators |20 and |42. Instead oflusing this'controlrmeans we may eifeot a transfer of streams` from product lines to slop lines directly by control means I2I, by` temperature controlledmeans responsive to atemperature increase in the fractionating column or n This introduction of renery gases is essential in by other change in operating conditions. The choice of the means of automatically diverting the various streamsto slop may depend to some extent on the time lag desiredbetween the time the reactor is by-passed and the time'the stream are Idiverted to slop. t

About 2000 barrel'sper clay of 39.3 A. P. I. gasoil is taken overhead throughline 95 but in view ofv theV absence oiligliter gases the pressure will fall below 5 pounds per square inch so thatfthevalve inline H9 will open to permitthe introductionV of reiinery gases into this stream.

order to protect compressor'- I `04, i. e., to provide a. t positive pressure on the compressorinlet `sothat the-compressormay continue to operate. As

soon as convenient valve |46 in by-pass line |41 is opened,y either-manually or automatically, so that the introduction of'refinery gases from line f I I9 may be stopped. The 2|l00"barrels` per day of 39.3 A. P. Lgas oil is diverted to slop through line I4I. i

The increased temperatures in heat exchangers I3, I4 and I5 cause the charging stock to be pre heated to a temperature of about 550 F. in this by-pass operation (during normal operation itis only heated to about 450' F.). This rise in the temperature of the preheated charging stock effects a decrease in the heat intensity in the furnace by closing valve |48 in fuel line |49 by suitable temperature controlled means |50.

While we have described in detail Vthe normal operations and by-pass operations of our system itwill be understood from the above description that the change-over from normal operation to by-pass operation is suiiiciently gradual that no undue strain is imposed on any part of the system. Some or all of the control means may be automatic but if the initial control means are automatic sufiicient time will be allowed for operators to attend tothe remaining control means. The control means per se form no part of our present invention and since they are well known in the art they will not be described in greaterl detail.

When our system resumes normal operation and the liquid levels tend to drop in the fractionating column, by-pass lines |28 and |45 will automatically be closed and the system will of its own accord readjust itself to the normal operating conditions. We prefer, however, to discharge product streams to slop tanks for suiilcient length of time after the normal operation has been resumed to avoid any possible contamination of product streams.

Referring once more to the reactor system we havev described the use of standpipe 39 when iunnel-shaped top 23 was used in the reactor. The use of standpipe 39 offers the advantage of means for controlling the amount of catalyst in the reactor. standpipe 39'- may be used for this purpose even when the funnel-shaped top 23 is employed. VIf the pressure at the baseV of standpipe 39' is not sufiiciently great, however, we may withdraw catalyst from the base'of `the reactor through standpipe 3S, piel:- it up with steam from line |52 to the upper settling chamberor hopper 26 which supplies standpipe 39.

If the amount of catalyst removed with reacnon vapors through, une 31 "is insumcient' for maintaining the pipe still coils free from carbon, additional catalyst from standpipe |53 aerated by steam from line |54 may be discharged through valve |55 and conveyed by steam from line |56 vthrough line |51 to the base` of column.

While we have described in detail aspeciiic example of our invention it should be understood that this example is by way of illustration and not by way of limitation. .Wide variations are permissible in operating conditions and in the heat balance throughout the system. Various modifications of the system and alternative arrangements will be apparent to those skilled in theart `from the above detailed description. Our invention is not, therefore, limited to any details hereinabove described except insofar as defined by the following claims.

.We claim: v, n i

1.-k In a hydrocarbon conversion system, a heater, a reactor, a fractionating column, a first heat exchanger, a rst cooler, means for withdrawing a liquid from the bottom of said column and for passing it through said heat exchanger and cooler and then for returning it to said column, a second -heat exchanger, a secondA cooler, means for withdrawing an intermediate stream from said column, for passing it through said second heat exchanger and said second cooler and for returning it to said column, a third heat exchanger, a third cooler, means for withdrawing liquid from an upper part of the tower and for and convey it through line .through said third heat exchanger, second heat exchanger, rst heat exchanger, heater, reactor and fractionating column, means responsive to the temperature of the charging stock entering .the heater for controlling the extentA of the heating in said pipe still, by-pass means for introducing hydrocarbons directly from said heater to said column, a liquid level controller in the lower part of the column, means for by-passing said rst cooler when a predetermined liquid level is exceeded in the lower part of the column, a liquid level indicator at an intermediate point in the tower, and means for by-passing said third heat exchanger and cooler when a predetermined liquid level is exceeded at the intermediate point in the tower.

2. The system of claim 1 which includes product lines and slop lines for Awithdrawing fractions from said column and means for closing said product lines and opening said slop lines during by-pass operation. v y

3. A hydrocarbon fractionation system capable of continuous operation when the vapors charged thereto aresuddenly changed from hot vapors of the gasoline boiling' range to hotter vapors ofthe gas oil boiling range and vice versa which system comprises a fractionating column, means for introducing vapors at a low point in said column, means Vfor quickly changing from one vapor charge to the other, 'a first cooler, means for withdrawing liquid from the upper part of said column, for passing said liquid through said first cooler and for returning said liquid to a still higher point in the column, means for bypassing said iirst cooler whereby a large proportion of the liquid withdrawn from the upper part of the column may be returned thereto -without passing through said rst cooler, a trapout pan at an intermediate point in said column, means in said by-pass for `controlling the amount of liquid flowing therethrough in accordance with the liquid level in said trapout pan, means for withdrawing liquid Vfrom said trapout'pan, means including a second cooler for cooling said with- Y drawn liquid and for returning a part of the cooled liquid to said column, a third cooler, means for withdrawing heavy liquid from the base of said column, for passing said vheavy liquid through said thirdcooler and for returning said cooled heavy liquid to said column at a point above the vapor inlet thereto, means for bypassing said third cooler, a valve inv said by-pass means for regulating the amount of liquid passing'therethrough in accordance with the liquid level in the lower part of the column and separate means for withdrawing heavy liquid from the system when the liquid level in the lower part of the column exceeds a predetermined level.

4. The system of claim 3 which includes means for withdrawing a side stream from said column above said trapout pan and belowv the upper liquid withdrawal, means for stripping said withdrawn side stream, and for returning the stripped material to said column, and means for with-v a hydrocarbon charging stock in series through -said first, second and third heat `exchangers,

means for passing liquid Withdrawn from the upper part of the tower through said rst heat exchanger, means for passing liquid lWitlfidrawn l ture, introducing intothe uid at af mixingl zone s a catalyst in a continuous uninterrupted flow at an effective pressure above the pressure of the fluid, normally 'passing the uid and catalyst" from the mixing zone `to a reacting zone and the hydrocarbon producttherefrom to a fractionating zone and byxpa'ssing the uid `around the mixing zone and reacting zone to the fractionating zonewhenfffntfi Jeffective pressure off the l0 catalyst is less ,tha a predetermined minimum.

WAYNE c. EDMIS'I'ER. -DoYoN H. PQLLOCK. 

